Catalyst for the polymerization of conjugated diolefins



United States Patent Oihce 3,471,461 Patented Oct. 7, 1969 US. Cl. 260-943 11 Claims ABSTRACT OF THE DISCLOSURE Conjugated diolefins such as butadiene and piperylene are polymerized with a catalyst system made up of either a titanium trichloride or tribromide, a Group III-IV metal iodide and a Group I-III alkyl or alkyl metal hydride.

The present invention relates to catalyst systems and their use for the formation of polymers of conjugated diolefins. More particularly, the invention deals with the polymerization of conjugated diolefins with a catalyst system made up of a titanium compound having a valence less than 4, a Group III-IV metal iodide and a Group I-III metal alkyl.

The polymerization of conjugated diolefins with various types of catalyst systems is well known in the art. Prior methods for the formation of polydiolefins have involved the use of catalyst systems made up of titanium tetrachloride, lithium aluminum alkyls and free iodine or an alkyl iodide as is disclosed in German Patents Nos. 1,157,787 and 1,157,788. Additionally, stereoregular polydiolefins have been formed with catalyst systems wherein a titanium iodide compound is a major ingredient (see Belgian Patents Nos. 629,626 and 631,730).

Now, in accordance with this invention, it has been found that tough, elastic materials having molecular weights in excess of 200,000 that are soluble in most organic solvents and free of crosslinking can be prepared with a catalyst system made up of a titanium trior dihalide, a Group III-IV metal iodide and a Group I-III metal alkyl or alkyl metal hydride.

Suitable conjugated diolefins useful for the preparation of the stereoregular, high molecular weight polymers of the invention include straight and branched chain adiphatic conjugated diolefins having preferably from 4 to 8 carbon atoms, and more preferably, from 4 to 5 carbon atoms. Representative non-limiting examples of useful 0.; to C aliphatic conjugated diolefins are: butadiene-l,3, pentadiene-1,3, isoprene, hexadiene-1,3, heptadiene-1,3, and octadiene-l,3. The preferred conjugated diolefins are butadiene-1,3 and pentadiene-1,3 also known as piperylene, because these materials are commercially available in large quantities at relatively low cost.

The solvents or diluents used in making the polymers of the present invention should be liquids at the conditions of temperature and pressure used in the polymerization reaction. Solvents suitable for use in the polymerization reaction include C to C saturated aliphatic hydrocarbons, such as butane, pentane, n-heptane, isooctane, n-decane, cyclohexane, methylcyclohexane, etc. The preferred solvents for use in the present polymerization process are aromatic compounds such as benzene, toluene, xylene, etc.

The catalyst system employed in preparing the polymers of this invention comprises at least three initial components; namely: a primary catalyst component, a dispersant medium, and a co-catalyst. The primary catalyst component is a reducible titanium chloride or bromide or a mixture of such compounds wherein the titanium is in a valence state of 3 or less. Particularly preferred catalyst components of this type are titanium trichloride, titanium tribromide, titanium trichloride cocrystallized with a Group I-III metal halide such as aluminum chloride, titanium dichloride and titanium dibromide.

The dispersant medium component of the present catalyst system is an iodide of a metal selected from Groups III-B and IV-B of the Extended Periodic Table of the Textbook of Chemistry, Mack et al., 2nd Edition, Ginn and Company, page 313, or a mixture of such iodides. Representative examples of useful metal iodides include A11 Gal SnI and InI Aluminum iodide is particularly preferred as the dispersant medium in the present catalyst composition.

The co-catalyst component of the catalyst system employed in this invention comprises a Group I-III metal alkyl or metal alkyl hydride. Particularly valuable as co-catalysts are the lower alkylaluminum compounds, especially trialkylaluminum compounds, lithium aluminum alkyl compounds, zinc alkyl compounds, as Well as alkylaluminum hydrides, lithium aluminum alkyl hydrides, and zinc alkyl hydrides. The preferred co-catalysts are the trialkylaluminum compounds having from 2 to 6 carbon atoms per alkyl group, such as triethylaluminum, tripropylaluminum, triisobutylaluminum, and the like, as well as the lower dialkylaluminum compounds such as diethylaluminum hydride, dipropylaluminum hydride, and diisopropylaluminum hydride.

The primary catalyst component and the dispersant medium of the catalyst system are preferably intimately contacted with each other in an inert environment prior to their use in the polymerization reaction. This intimate contacting can be carried out either by fusing the catalyst dispersant medium mixture at a temperature above the melting point of the dispersant medium or by intensely milling the mixture for a period of time sufficient to cause substantial dispersion of the primary catalyst component in the dispersant medium.

The period of time needed for the latter operation will, of course, depend greatly upon the efficiency of the milling equipment. Thus, for ball mills employing steel balls as the grinding medium, a milling period of from 2 to about 10 days will usually be sufficient, while for ball mills employing less dense grinding media longer milling periods may be required for satisfactory results. Conversely, highly satisfactory results may be obtained in a much shorter period of time when mills are utilized in which centrifugal or other non-gravity force is allowed it 1. i461 J to act upon the grinding medium, as is the case in certain modern vibrating or swinging milling equipment.

The fused or ball milled mixture of primary catalyst component and dispersant medium is preferably mixed with the co-catalyst in an inert organic diluent prior to their use in the polymerization system. Alternatively, the fused or milled mixture and the co-catalyst can be mixed or added individually to the reactants in the absence of any diluents.

The molar ratio of dispersant medium to primary catalyst component can vary in the range of from about 0.5 :1 to about 10:1, preferably 1:1 to 5:1. The molar ratio of alkyl groups in the co-catalyst to iodine atoms in the dispersant medium is of a critical nature and should be so adjusted that the ratio between the alkyl groups in the co-catalyst and the iodine atoms in the dispersant medium will be between about 1.4 and 3, preferably about 2, when the metal valance in the dispersant medium is 3, and between about 1.5 and 4.5, preferably about 2.3, when the metal valence in the dispersant medium is 4.

It has been found that if the molar ratio of alkyl groups in the co-catalyst to the iodine atoms in the dispersant medium is less than or greater than what is indicated by these two ranges, little or substantially no polymer is formed. Since trialkylaluminum is a very reactive compound, which readily reacts with numerous other compounds and elements, it may, of course, be possible to use catalyst systems in which the original alkyl to iodine ratio is higher than about 3 and 4.5, respectively, by adding a fourth reactive component which would partly remove or neutralize the catalytic influence of the excess trialkylaluminum. However, such systems, if at all practical, would fall within the scope of this invention. Likewise, when significant amounts of reactive impurities, such as water, alcohols and oxygen, are present in the system, the optimum alkyl/iodine ratio may be correspondingly higher.

The total amount of catalyst employed in the polymerization reaction varies with the choice of components of the catalyst system and with the type of monomer polym erized, but is generally in the range of from about 0.005 to about 0.3 wt. percent, preferably 0.01 to 0.1 wt. percent, based upon the total reaction mixture comprising the monomers to be polymerized and the reaction diluent.

The conditions at which the polymerization reaction is conducted can vary over a wide range. Generally, temperatures ranging from less than to about 100 C. can be used; however, temperatures ranging from 15 to 70 C. are preferred. Pressures ranging from subatmospheric to about 10 atmospheres, depending upon the vapor pressures of the diolefin and diluent, can be employed in the polymerization reaction. The reaction times used in the formation of the preferred polymers depend in general upon the temperatures and catalyst concentrations used. Reaction times ranging from 5 minutes to 200 hours can be employed; however, it is more usual to use reaction times ranging from about 5 to 72 hours.

The reaction vessel used for the polymerization can be constructed of any material that is inert to the reactants used, and is capable of withstanding the operating pressures. Reactors made of glass, stainless steel and glasslincd steel may thus be used.

In a typical preferred embodiment of a complete polymerization procedure, a nitrogen blanketed reaction flask equipped with stirrer and reflux condenser is first charged with titanium trichloride and purified anhydrous aluminum iodide. The molar ratio of aluminum iodide to titanium trichloride can suitably vary from about 1:1 to 5 :1. The glass reaction vessel is then heated to a temperature in the range of 280 to 320 C. which causes the aluminum iodide to melt at about 191 C., at which time stirring of the reaction mixture is commenced. After a period varying from about 2 to hours, the heating of the reaction vessel is stopped, the mixture cooled and a solidified product is recovered in essentially quantitative yield.

The fusion product of titanium trichloride and aluminum iodide is then introduced to a reaction vessel containing benzene and is contacted with triethylaluminum. The molar ratio of triethylaluminum to aluminum iodide in the catalyst mixture is adjusted at a value of about 2.

The total catalyst mixture is then introduced into a glass reaction vessel containing a C to C conjugated diolefin in benzene, whereupon the total reaction mixture is agitated under the autogenous pressure of the monomer and diluent for a period ranging from 24 to 48 hours at a temperature varying from 25 to 60 C. In operating the polymerization process, in general, all of the diolefin may be present before the catalyst is added; alternatively, part or all of the diolefin may be added during the polymerization. This introduction may be continuous, or intermittent.

The amount of catalyst used for the formation of the polymers of the present invention varies from about 0.01 to 0.5 part of catalyst per parts of monomer. Upon completion of the polymerization reaction, the polymerization catalyst is deactivated by the addition of a small quantity of lower alkanol. The polymer product is recovered from the reaction mixture by the use of lower alkanol precipitation or solvent evaporation.

The polymers of the present invention exhibit molecular weights ranging from 10,00 to 3,000,000, and are generally in excess of 200,000. Molecular weight of the polymers is determined by the method of Johnson and Wolfangel, Industrial Engineering Chemistry, 44, 752 (1952). In the case of polybutadienes, the polymers contain from about 40 to 99% cis-l,4-unsaturation. The polymers of this invention are rubbery in nature and may be cured to form highly useful rubbers. Any one of a wide variety of curing procedures may be employed, such as sulfur curing or free radical curing. My of the procedures familiar to those skilled in the processing of established elastomers such as natural rubber, butadienestyrene rubber (SBR), and butyl rubber are suitable.

The polydiolefins of this invention have many varied uses. They may be employed in the preparation of tires, inner tubes, hose and tubing, wire and cable coatings, as

' well as for a wide variety of coated or molded articles.

This invention and its advantages will be better understood by reference to the following examples:

EXAMPLE 1 A series of tests were made to illustrate the effectiveness of the catalyst system of the present invention for the polymerization of conjugated diolefins. In every instance, the test was carried out in a 1-liter glass reaction vessel which was agitated by being placed on a paddle wheel stirrer in a temperature controlled water bath.

The reaction system was made up of 500 mls. of benzene and 100 grams of conjugated diolefin. To this mixture of diluent and monomer was added the catalyst in the amounts specified in each of the runs. After the completion of the polymerization reaction, a small amount of dry isopropanol was added to the reaction vessel to deactivate the catalyst. Following the deactivation, the total contents of the reaction flask were poured into an excess of isopropanol.

In the runs wherein a fused catalyst component is specified as being used, the catalyst was prepared by fusing the primary catalyst component and the dispersant medium at the temperature specified for a period ranging from 0.4 to 50 hours. The results of the test are set forth in Table I below.

TABLE I Type TlCla.5A1Ia- TiCla.5AlI3 Method of preparation e1 d Fused Melt. Temp of preparation 320 Weight (mg.) Ti halide content (mmois Activator: Type Weight (mg) Al compound/Ti compound (mole ratio) /1 ratio u Diolefin type Reaction conditions;

Temperature C.) Run length (hrs.) Results High moi. wt. polymer (g.) Moi. wt.Xi0-

Unsaturation, percent of total:

Type I Type II, trans Type II, ciq Gel, percent 1,2 addition, percent Run Catalyst:

Type TiC Mm TiC HAW TiCh HAIL TiC HAIL TiCi3.5A1I3 TiCl3.3AlI3 Method of preparation Temp. of preparation C.). Bali mill time (days)- Weight (mg.) Ti halide content (mmols) Activator:

eight (mg) 75.4- 71.4. 107.1 53.6-.- 286 386 Al conpound/Ti compound (mole ratio) 15. re 10 Reaction conditions:

Temperature 0.) Run length (hrs.)-

Results:

High moi. wt. polymer (g.) 0.....

M01. wt.X10' b Unsaturation, percent of total:

yp I Type II, trans Type II, cis

Gel, percent 1,2 addition, percent Catal st:

Type Til-z TiI3. Til; TiCla.2SnI TiC1a.2Si1I4. a-TiCh Method of preparation Dry Milled-.. Fused Melt... Temp. of preparation C.) 25 144 Ball mill time (days) 6--.. 0.04. 0 Weight (mg.) Ti halide content (mmols) 0.125 Activator:

Type Weight (mg.) Al compound/Ti compound (mole ratio) R/I ratio Diolefin, type Butadiene Reaction conditions:

Temperature C.) 60 Run length (hrs.) 24 24 Results:

High moi. wt. polymer (g.) 2.1 M01. wt. (i0 b Unsaturation, percent of total:

yp T Type II, trans Type II, cis Gel, percent. 1,2 addition, percent Footnotes at end of table TABLE I-Continued Run Catalyst:

Type a-TiCls TiCl;.AlI3 TiCla.2AlIa.- TiCla.3AlI; TlCl3.3AlIa TiCl3.2SnI4 Method of preparation Weight (mg) Ti halide content (mmols) Activator:

Type

Weight (mg.)

Al compound/Ti compound (mole ratio) R/I ratio Diolefin, type Butadiene... Reaction conditions:

Temperature C.) 25 60 60 60 60 60 Run length (hrs.) esults:

Unsaturation, percent of total:

Type I 4.3 Type II, trans. Type II, eis.

Gel percent 0 1,2 addition, percent 40 36 37 e Includes Al in both Al(C2H5)a and A113. (msglnherent viscosity determined in toluene solution at 25 0.; MW determined from correlation of Johnson & Wolfangel, Ind. Eng. Chem., 44, 762 s R/I designates the molar ratio of the moles of alkyl groups present in the activator to the moles of iodine atoms present in the dispersant medium. d (AH-Sn)/Ti ratio.

The results of Runs 1 through 5 indicate that the tita- 24 hours in order to secure thorough dispersion or conium trichloride, aluminum iodide, triethylaluminum catcrystallization of the compounds. alyst system of the present invention serves to promote The fused titanium trichloride-aluminum halide mixture high yields of cis-1,4-polybutadiene. In each of the first Was then activated with an amount of triethylaluminum five runs the conversion of butadiene-1,3 to polybutadiene sufiicient to secure a ratio of triethylaluminum to alumiwas in excess of about 90% and the polymer so formed num halide of about 2, whereupon the catalyst mixture had molecular weights of at least 200,000 and above. was introduced into a reaction flask containing 100 grams Runs 6 through 12 illustrate the criticality of maintainof butadiene-1,3 and 500 this. of benzene diluent. The ing the molar ratio of the alkyl groups in the activator catalyst, monomer and diluent were maintained at a temto the moles of iodine atoms in the dispersant medium perature of 60 C. with stirring for a period of 24 hours. when aluminum triiodide is the dispersant medium at a At the completion of the reaction period, the polymer value between about 1.4 and 3. When the molar ratio produced was isolated from the reaction mixture with dry of alkyl groups in the activator to iodine atoms in the isopropyl alcohol, dried, weighed and analyzed for cisaluminum iodide dispersant medium is less than or exceeds 40 1,4 unsaturation. The molecular weight of the product so the range specified, substantially less high molecular formed was determined ac ordin to the method of Johnweight polymer is formed. son and Wolfangel, Industrial Engineering Chemistry, 44, Runs 13, 14, 15, 18 and 19 indicate that neither titan 752 (1952). Inherent viscosity measurements were made um triiodide nor titanium trichloride when activated with in tolu n at 25 C, Th lt f th t t are t f -th diethylaluminum iodide is equivalent to the catalyst sysi T bl IIb 1 tern of the present invention for the polymerization of 4 TABLE II conjugated diolefins. In each of these runs, none or substantially no high molecular weight polymer was formed. Titanium compmmt MOL wt C154 4 Runs 16 and 17 illustrate the applicability of stannic Composition mmoles Yield, g. X10 percent;

iodide for use as the dispersant medium in the catalyst system of the present invention. The catalyst mixture of 1' 'r cnzan, 0.0625 33.7 920 93.2

titanium trichloride, stannic iodide and triethylaluminum gig ggg 3;;

served in promotlng the formation of substantial quan- TiChJAlCl; 0.125 Trace tities of high molecular weight polybutadiene. 6" :gighgfi g g: 1 g 3g 25:: Runs 20, 21, 22 and 24 illustrate the applicabihty of T1013.3A1C1z 0.125 0.2

the catalyst system of the present invention for the polymerization of piperylene to high molecular weight poly- The results of the runs set forth in Table H above inpiperylene having a high degree of trans-unsaturation and dicate that aluminum bromide and aluminum chloride are 1, 2 addition. Run 23 illustrates the criticality of mainnot suitable as dispersant media in the catalyst system of taining the ratio of activator to dispersant medium at the present invention. In contradistinction, aluminum ioabout 2 when piperylene is the monomer to be polymerdide serves to promote the formation of high yields of high ized. molecular weight polybutadiene. Runs 4, 6 and 7 demonstrate that when aluminum chloride or aluminum bro- EXAMPLE 2 mide are used in conjunction with triethylaluminum and To illustrate the criticality Of utilizing metal iodides as titanium trichloride, only small amounts of polybutadiene the dispersant medium in the catalyst system of the presare produced d that th polymer f d ha a l tively ent invention, a series of polymerizations were conducted l molecular i h in which various aluminum halides were used as the dispersant media for titanium trichloride. A fusion of the EXAMPLE 3 titanium trichloride component and the aluminum halide To demonstrate the criticality of the use of a titanium was prepared by contacting the two components at a tem- 7O trihalide as a catalyst component in the instant threeperature above the melting point of the aluminum halide component catalyst system, a series of butadiene polymin a sealed tube inside a rocking steel bomb. When aluerizations were conducted with other transition metal haminum chloride was used as the dispersant medium, two lides in combination with aluminum iodide and triethylsuch reaction periods were employed with intermediate aluminum. The transition metal halide-aluminum iodide grinding of the mixture with chrome alloy steel balls for mixtures were formed by steel ball milling the compo nents for a-period of 6 days at a temperature of about 25 C. Each of the catalyst mixtures was activated with an amount of triethylaluminum sufficient to obtain a molar ratio of triethylaluminum to aluminum iodide of about 2. The total catalyst mixture was then introduced into a The above data indicate that the polypiperylene samples formed with the catalyst system of the present invention are readily sulfur-cured to vulcanizates having moderately high tensile strengths. It should be recognized, of course, that the polypiperylene vulcanizate tensile l-liter glass reaction vessel containing 100 grams of butastrengths may be improved by blending the polymer with diene-1,3 and 500 mls. of benzene. The entire reaction materials such as polybutadiene, styrene butadiene rubmixture was maintained at a temperature of 60 C. with her, and natural rubber. agitation for a period of 24 hours. At the completion of Further advantages of this invention will be apparent the reaction period, the polymer was isolated from the to those skilled in the art. Polymers of conjugated diolereaction mixture with dry isopropyl alcohol, dried, weighfins that are readily sulfur-curable can be conveniently ed, and tested for Type II cis unsaturation. The molecuand efliciently prepared with the catalyst system of the lat weight of the polymer was determined according to present invention. It is to be understood that this inventhe method enunciated in Example 1. The results of the tion is not limited to the specific examples set forth heretest are set forthinTable III below. in, which have been offered merely as illustrations, and

TABLE III TiCl3.A1I3 voumra CXC13.A1I3

Transition Metal Component:

MCl3.AlI3, mmoles 0. 0.125 0.125 AI(C2H5)3, mmoles 0. 5 0. 25 0.25 R/I ratio 2 2 2 Yield, g 89. 8 Trace 0 Anaylses on Polymer:

Mol. wt.X10- 380 ype II cis unsaturation, percent 89. 3

T e M stands for the transition metal.

the moles of iodine atoms perseut in the dispersant medium.

From the data set forth above, it is apparent that other transition metal chlorides such as vanadium trichloride and chromium trichloride are not equivalent to titanium trichloride in the catalyst composition of the present invention. Neither vanadium trichloride nor chromium trichloride when used in combination with aluminum iodide and triethylaluminum serves to form an appreciable yield of polybutadiene. In contrast, titanium trichloride in combination with an aluminum iodide dispersant medium and a triethylaluminum activator served to secure an 89.8% yield of polymer having a molecular weight of 380,000.

EXAMPLE 4 To demonstrate the curability of the polypiperylene polymers formed with the catalyst system of the present invention, two samples of polypiperylene having differing molecular weights and type and degree of unsaturation were compounded on a rubber roll mill with 50 grams of high abrasion furnace black, 1 gram of phenyl fl-naphthylamine, 2 grams of stearic acid, 3 grams of zinc oxide, 1.75 grams of sulfur, 1 gram of N-oxydiethylene-Z-benzothiazolesulfenamide, and 0.25 gram of di-Z-benzothiazyl disulfide per 100 grams of polypiperylene. The stocks thus obtained were heated at a temperature of 307 F. for varying lengths of time in a mold to give cured rubbery slabs. The slabs were subsequently cut into standard dumbbells and tested under ASTM conditions of temperature and humidity on a Scott micro-tensile tester. The results of the tensile test for each of the two polypiperylene samples are set forth in Table IV below.

TABLE IV Sample Cure time: 10 min.:

Tensile, p.s.i 3, 030 2, 750 200% modulus, p.s.i 300% modulus, p.s.i 930 Elongation, percent 840 770 Cure time: 20 min.:

Tensile, p.s.i 3, 410 3,060 200% modulus, p.s.i c 930 800% modulus, p.s.i 1, 890 Elongation, percent 49 Cure time: min.:

Tensile, p.s.i 200% modulus, p.s.i 300% modulus, p.s.i Elongation, percent Polymer characteristics:

M01. wt. 10- 375 290 Type II trans-unsaturation, percent 75. 5 70. 0 1,2addition, percent 38 that modifications may be made without departing from the spirit and scope of the appended claims.

What is claimed is:

1. A catalyst system for the polymerization of conjugated diolefins which comprises an inorganic titanium halide compound, said titanium moiety having a valence less than 4, a Group III-B to IV-B inorganic metal iodide intimately contacted by fusing or intensely ball milled with said inorganic titanium halide, the molar ratio of inorganic metal iodide to inorganic titanium halide varying from about 0.5:1 to about 10: 1, and a Group I-IH metal activator compound selected from the group consisting of Group I-III metal alkyls and Group I-III metal alkyl hydrides, the molar ratio of alkyl groups in the activator compound to iodine atoms in the inorganic metal iodide varying from about 1.421 to 3:1 when the metal moiety of the inorganic metal iodide has a valence of 3 and from 1.5 :1 to 4.5 :1 when the metal moiety of the inorganic metal iodide has a valence of 4.

2. The catalyst system of claim 1 wherein said inorganic titanium halide compound is selected from the group consisting of titanium trichlorides, tribromides, dichlorides and dibromides.

3. The catalyst system of claim 1 wherein said Group I-III metal activator is an alkyl aluminum compound.

4. The catalyst system of claim 1 wherein said Group III-B to IV-B metal iodide is selected from the group consisting of A11 and SnI 5. The catalyst system of claim 1 wherein the inorganic titanium halide compound is titanium trichloride, the inorganic metal iodide is aluminum iodide, and the metal activator is triethyl aluminum.

6. The catalyst system of claim 5 wherein the molar ratio of alkyl groups in the triethyl aluminum to iodide atoms in the aluminum iodide is about 2: 1.

7. A process for polymerizing conjugated diolefins which comprises contacting a C to C straight chain, conjugated diolefin in a hydrocarbon diluent with a polymerization catalyst comprising an inorganic titanium halide compound, said titanium moiety having a valence less than 4, a Group III-B to IV-B inorganic metal iodide intimately contacted by fusing or intensely ball milled with said inorganic titanium halide, the molar ratio of inorganic metal iodide to inorganic titanium halide varying from about 0.5 :1 to about 10:1, and a Group I-III metal activator compound selected from the group consisting of Group I-III metal alkyls and Group I-III metal alkyl hydn'des,

the molar ratio of alkyl groups in the activator compound to iodine atoms in the inorganic metal iodide varying from about 1.4:1 to 3:1 when the metal moiety of the inorganic metal iodide has a valence of 3 and from 1.5 :1 to 45:1 when the metal moiety of the inorganic metal iodide has a valence of 4, and recovering a polymerized polydiolefin from the polymerization reaction mixture.

8. The process of claim 7 wherein said Group I-IIl metal activator is a lower alkyl aluminum compound.

9. The process of claim 7 wherein said Group III-B to IV-B inorganic metal iodide is selected from the group consisting of AlI Gal SnI and InI 10. The process of claim 7 wherein the straight chain, conjugated diolefin has from 4 to 5 carbon atoms.

11. The process of claim 10 wherein the inorganic titanium halide compound is titanium trichloride, the inorganic metal iodide is aluminum iodide, and the metal activator is tn'ethyl aluminum.

References Cited UNITED STATES PATENTS Naylor 260-943 Edmonds et al. 260-429 Porter et a1 260-429 Tornqvist et al 260-429 Balas 260-429 Tornqvist et a1 260-429 Bonner -1. 260-429 Farrar et a] 260-943 Rindtorfi et a1. 260-429 Zelinski 260-943 Zelinski 260-943 U .8. Cl. X.R. 

